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PERCENT OCCURRENCE IN WHICH VSS WAS EQUAL TO OR LESS THAN THE STATED VALUE
-------
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-------
Analysis of waste constituents indicated the following geometric mean concentrations:
Parameter Concentration (mg/1)
BOD 1,850
COD 8,200
VSS 800
Phosphate (as PO4) 8.6
The BOD and COD values were considerably higher than those for the domestic waste. Since
the COD and BOD were not filtered, the results reflected oxygen demand due to both
soluble organics and suspended solids in the wastewater. The high volatile suspended solids
were due primarily to the presence of cellulose fibers in the pulp and paper mill wastewater.
The relatively high BOD of the NSSC wastewater and low BOD of the clarified domestic
wastewater resulted in high industrial process loadings to the pilot system. Table 4 shows a
comparison of hydraulic loadings and corresponding process loadings. The basis for the
comparison was the geometric mean BOD for the NSSC wastewater and the municipal
wastewater, or a 1,850 and 135 mg/1 BOD for the industrial and domestic wastewaters
before blending. It can be seen that on the basis of equal hydraulic loadings that a
considerably higher industrial process loading is handled by the plant.
The other constituents fall in the following ranges:
Constituent Concentration (mg/1) *
pH 6.3 - 7.7
Total Solids 7,670 - 18,300
Settleable Solids 10-900
Temperature (° C.) 17-41
Ammonia Nitrogen (as NH3) nil 35.0
Nitrate Nitrogen (as NO3 ) nil - 40.0
Organic Nitrogen (as N) 9.8 - 194.0
*Except pH and temperature
It is seen that the wastewater temperature and pH did not vary appreciably due to
consistent operation of the paper mill process (see Table A-2 in the Appendix). In addition,
there were no reported incidents during the study of accidental spills which could have
upset the pH. Nitrogen levels were more than sufficient to satisfy nutrient requirements.
Color data from laboratory studies indicated the raw NSSC waste had a color of 24,000
APHA units. At this color level, the waste was very dark brown and extremely turbid.
29
-------
TABLE 4
COMPARISON OF HYDRAULIC
AND PROCESS LOADINGS
Hydraulic Loading
Percent of Total
NSSC
Wastewater
Clarified
Domestic
Wastewater
Process Loading
Percent of Total
NSSC
Wastewater
Clarified
Domestic
Wastewater
1
10
50
75
90
99
90
50
25
10
12
42
93
98
88
58
7
2
30
-------
In summary, wastewater characterization indicated relatively high concentrations of volatile
suspended solids, BOD and COD, and showed an adequate amount of phosphorus and
nitrogen nutrients for biological treatment. The pH was within limits for biological
treatment (6 to 9), but the color was very dark.
31
-------
SECTION VII
PRIMARY TREATMENT OF NSSC WASTEWATER
The primary treatment of the raw NSSC wastewater was accomplished by settling the pulp
and paper solids and removing the sludge from the primary clarifier. The unit was operated
throughout most of the study from February, 1971, to March, 1972, and its performance
was based upon an evaluation of some of the operational data described in the following
subsections.
Operation
The raw NSSC wastewater flowed from the influent weir box by gravity through a four-inch
cast iron pipe. The flow depended upon the pilot unit's requirements and was controlled by
a throttling valve. Sludge was collected by rakes in the hopper bottom clarifier, and it was
withdrawn periodically through an eight-inch pipe at the bottom of the clarifier to the waste
sump. At times during the study, heavy fiber paper solids created plugging problems and
caused some solids carry-over in the final effluent.
Normally, the raw NSSC wastewater had high concentrations of suspended paper solids (350
to 4,500 mg/1). In addition, there were considerable amounts of unsettleable dissolved and
suspended volatile solids which contributed to the total BOD and COD of the wastewater.
The temperatures were usually higher than the domestic wastewater and did not fluctuate
significantly with ambient temperature changes. This was due to the constant operation of
the pulp and paper mill and as a result, temperature was not a major consideration in
evaluating the efficiency of the clarifier.
Grab samples were collected at the sample points shown in Table 1 and Figure 2. An
evaluation of the data from the influent sample point from May, 1971, through September,
1971, resulted in a change in location of that sample collection station. For that time
period, the samples were collected at a location which gave erroneously high suspended
solids results. To remedy this, the sampler was changed to a more suitable location for the
balance of the study.
Performance
Performance of the primary clarifier was based upon the removal of BOD, COD and VSS at
various overflow rates, detention times and solids loading rates. The primary settling data
are averaged and summarized in Table 5; the individual data are given in Tables A-2 and A-3
of the Appendix.
32
-------
TABLES
PRIMARY TREATMENT DATA - NSSC WASTE MONTHLY AVERAGES*
Month
October
November
December
January
February
March
Average
Flow
(GPD)
22,000
16,600
28,600
26,500
23,400
17,400
22,400
Influent
Volatile
Suspended
Solids
(mg/1)
1,370
925
1,385
665
865
440
940
Percent Removal1
by Sedimentation
Influent
BOD
{mg/D
1,620
1,945
2,050
1,890
1,825
1,635
1,825
Influent
COD
(mg/1)
9,145,
9,320
8,510
7,240
8,660
7,140
8,335
Water
Temperature
(°F.)
92
81
79
66
73
80
79
Volatile
Suspended
Solids
62
50
45
76
70
69
62
BOD
-17
-10
0
-21
-10
-9
11
COD
8
10
-5
-15
13
13
4
Detention
Time
(hr)
7.0
9.5
5.3
5.9
6.4
6.6
6.8
Sedimentation
Overflow
Rate
(GPSFPD)
254
192
330
306
270
201
254
Solids
Loading
(Ib/sq ft)
3
2
4
2
2
, 1
2
April and May data omitted due to plant start up
June to October data omitted due to change in sampling procedure
1 Negative values indicate increases in BOD and COD concentrations due to sedimentation
-------
The detention time and overflow rate calculations were based on the volume as calculated
from the sidewater depth and inside diameter of the clarifier. For example, an inflow of
22,000 gpd is calculated to give 6.5 hours detention time with an overflow rate of 254
gpd/sq ft. The corresponding weir overflow is 67 gpd/lin ft.
Evaluations based upon statistical analyses before and after clarification are shown
graphically in Figures 12, 14, 16 and 17. For BOD and VSS analyses of the influent and
effluent, the average values were determined as follows:
Geometric Mean (mg/1)
Percent
Parameter Influent Effluent Removed
BOD 1,950 1,700 13
VSS 800 450 44
A comparison based upon monthly average calculations (see Table 5) showed reductions of
62 percent for volatile suspended solids and an increase in BOD across the primary clarifier.
The COD was reduced an average of four percent and showed some decrease in organics.
The performance evaluations were difficult to determine due to variations in the data for
the different detention times and overflow rates. Inconsistent data were due partially to
solids overflow when the sludge drawoff line was plugged by paper fibers. Also, variations in
performance were caused by the high percentages of unsettleable solids which contributed
to the BOD and COD. The volatile suspended solids were reduced an average of 44 to 62
percent for the detention times and overflow rates tested.
34
-------
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CLARIFIED NSSC WAST
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tEATMENT OF DOMESTIC WA
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PERCENT OCCURRENCE IN *HICH BOOg WAS EQUAL TO OR LESS THAN THE STATED VALUE
-------
CO
CT>
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-------
SECTION Vffl
BIOFILTRATION
The biofiltration process unit included a high rate trickling filter packed with synthetic
media and an intermediate clarifier with recirculation. This unit was operated from October,
1971, through March, 1972. The performance was rated according to data collected from a
sampling program during this period.
Operation
For the first six to eight weeks of operation the biofilter developed a growth and was
allowed to acclimate to the wastewater. Samples were collected from sample points as
indicated in Table 1 and Figure 2. Only the data collected after the first six weeks of
operation was used in the performance evaluation. During the study the NSSC wastewater
percentage ranged from 70 to 100 percent. At the times when 100 percent NSSC
wastewater was used some tap water was introduced to assure proper operation of the
trickling filter distribution arm.
Performance
Table 6 provides weekly average operating data for the biofiltration process. Of particular
importance is the data on process loading. A comparison of normal high rate filter loading
and that experienced by the biofilter in this study is as follows:
Hydraulic Loading Organic Loading
Biofilter Description (mgd/acre) (Ib BOD/1,000 CF)
Normal High Rate Biofilter 10 - 30 80-100
Pilot Plant Biofilter 48-102 100-400
The data in Table 6 also shows the rather narrow temperature range the biofilter
encountered. For the period of data evaluation, the high temperature was 20° C. with an
average of 16° C. Due to the relatively narrow temperature range, the standard temperature
correction factor (Eckenfelder, 1966) for biofilters was not applied.
The BOD organic loading (pounds per day per thousand cubic feet filter media) was plotted
versus the BOD removed (ppd) as shown in Figure 18. This figure shows clearly that primary
treatment of the raw NSSC waste improved the BOD removal efficiency. As an example,
37
-------
oo
TABLE 6
BIOFILTER OPERATION DATA WITH PRIMARY TREATMENT
TcmDentim
Week of
10/I01
io/i7*
10/241
10/31 1
11/71
11/14
11/21
11/28
12/5
12/12
12/19
12/26
1/2
1/9
1/16
1/23
1/30
2/6
2/13
2/20
2/27
Average
°F.
_
79
77
73
66
72
66
64
66
68
66
66
55
68
63
59
52
54
54
54
59
62
°C
26
25
23
19
22
19
18
19
20
19
19
13
20
17
15
11
12
12
12
15
16
Process Loading
qb/day/l.OOOft3)
BOD COD
290 2
360
370
200
200
180
465 2
420
325
450
375
435 3
510
505
390
95
120
115
90
100
75
291
1,740
1,190
690
1,050
.6802
1.3402
1,680
1,250
1,460 2
1,110
1,470 2
1,480
1,240
1,190
335
305
345
300
345
230
923
Hydraulic
Loading
withRedrc.
(mdg/acre)
74
84
74
64
58
47
108
108
85
106
100
101
98
82
99
76
85
84
64
64
57
82
Recite.
Rate
(percent)
50
50
60
90
130
140
150
50
60
35
50
60
60
40
60
90
100
110
120
130
95
80
Removal
(percent) .
BOD
272
11
17
14
10
18,
*>
45
17
28
18
3,
242
3
16
8
18
9
18
11
14
-
16
COD
25
17
11
36
172
82
25
6°
282
2
242
4
10
_
122
1
7
13
12
-
14
Removal
(Ib pet day)
BOD
1152
60
95
40
30
45,
3102
130
135
120
20,
ISO2
25
95
45
25
15
30
15
20
-
74
COD
640
300
120
550
170,
ISO2
620
1,090
5902
40
S102
100
190
_
602
5
35
55
60
-
330
NSSC Content
of Combined
BOD
(percent)
70
66
73
83
72
69
66
76
82
83
80
74
90
83
81
89
96
97
100
100
100
82
WITHOUT PRIMARY TREATMENT
3/15
3/12
3/19
3/26
Average
57
63
63
63
62
14
17
17
17
16
275
253
230
280
260
890
990
1,030
890
950
89
106
90
89
93
50
50
65
65
60
9
18
15
11
13
13
19
32
14
20
35
70
50
45
50
270
310
490
190
315
80
71
77
90
79
'Period allowed for biofflter start up; data not used in evaluation
on a single day's data
-------
600
500
\
FTT
T--
-f4-4-+
-H-
400
300
200
I MAR*
GlR^AT
I.S.
1RAJI
NSSC
usz
Hi-
100
100
200
300
400
BIO-FILTRATION BOD,REMOVAL VS.
B005 REMOVED (Ib day) BOD$LOADING
TREATMENT OF DOMESTIC WASTEWATER
AND NSSC PULP AND PAPER MILL WASTES
33
FIGURE IB
-------
with primary treatment a 100 ppd removal could be achieved when the biofilter was loaded
with 400 pounds of BOD per thousand cubic feet of filter media. Without primary
treatment, the loading must be reduced to 160 pounds of BOD per thousand cubic feet to
achieve the same pounds BOD removed.
Figure 18 also shows that essentially no BOD removal took place where the NSSC
percentage was greater than 80 percent. This was independent of the total organic loading to
the biofilter.
The overall treatment efficiency of the biofiltration process can be seen in Table 6. On an
average the biofilter removed only 16 percent and 13 percent, respectively, of the influent
BOD with and without primary treatment of the raw NSSC waste. The low removal
efficiency (typical of a high rate "roughing" biofilter) was a result of the high organic and
hydraulic loading of the biofilter.
William Eckenfelder's, Manual of Treatment Processes, cited hydraulic loadings of biofilters
treating other pulp and paper mill process wastes ranging from 90 to 365 mgd/acre for the
Kraft Mill waste and 47 to 189 mgd/acre for black liquor wastes with no recycling. BOD
removal rates at those hydraulic loadings ranged from 10 to 31 percent for the Kraft Mill
wastes and from 58 to 73 percent for the black liquor wastes. The raw wastes in the studies
cited were diluted, as witnessed by the influent BOD concentration of 250 mg/1 and 400
mg/1 for the Kraft Mill and black liquor wastes, respectively.
Design criteria for operation of the biofiltration process can be taken directly from Figure
18. For example, to remove 100 pounds of BOD per day by biofiltration, it would be
necessary to load the biofilter at 400 ppd per thousand cubic feet of filter media.
The following conclusions can be made from the biofiltration evaluation:
1. The biofilter functioned primarily as a "roughing" filter at
the high hydraulic and organic loadings experienced.
2. The "roughing" filter function improved downstream process
efficiencies.
3. Primary clarification of the raw NSSC waste improved the
biofiltration efficiency.
4. The biofilter was not effective in removing BOD from the
combined wastewater with high percentages (greater than 80
percent) of NSSC wastewater.
40
-------
SECTION IX
EXTENDED AERATION TREATMENT
The extended aeration system of the pilot plant was comprised of an aeration basin with
diffused air and a final clarifier with sludge return. Operation of the system began in
February, 1971, and continued through March, 1972. The performance of the system was
evaluated by collecting data based upon a sampling and analytical program carried out
during the study. Variations in NSSC to domestic waste loading, hydraulic flows, aeration
detention times, temperature, primary treatment, etc., were achieved during the study. The
effects of these conditions on the extended aeration process were evaluated from an
operation and performance standpoint.
Extended aeration was studied in three different arrangements:
Arrangement No. 1 Pretreatment with primary clarification
Arrangement No. 3 Pretreatment with primary clarification
and biofiltration
Arrangement No. 4 Pretreatment by biofiltration
Finally, performance comparisons of each of the three arrangements were made; oxygen
data and sludge production design criteria were developed.
Extended Aeration with Primary Clarification Arrangement No. 1
The aeration basin was operated with primary clarification from July, 1971, through
September, 1971. During this period, the percentage of the wastewater loading which was
NSSC BOD loading ranged from 42 to 100 percent. In addition, attempts were made to
optimize the mixed liquor volatile suspended solids (MLVSS) at various flows and BOD
loadings. Since BOD loadings could not be determined immediately, flow control was the
primary means of varying the loadings.
Evaluation of the extended aeration process with primary clarification was based upon the
results summarized in Table 7. A comparison of BOD loading to effluent quality is given in
Figure 19. As can to be from this graph, there appeared to be no significant difference in the
effluent quality for the various percentages of the NSSC wastewater evaluated. It is believed
that the NSSC loadings (which were always greater than 42 percent of the wastewater) were
too high to provide a significant comparison of variation in efficiencies of extended aeration
with NSSC and domestic wastewater influents.
41
-------
to
TABLE 7
EXTENDED AERATION RESULTS - (JULY 14 - AUGUST 26,1971)
ARRANGEMENT NO. 1
Operating
Temperature
Date ( C.)
7/14/71
20
21
22
27
28
29
8/10/71
11
12
17
18
19
24
25
26
27
28
28
29
29
29
29
29
28
28
28
29
29
28
28
Percent NSSC
MLVSS Waste Based
(mg/0 on BOD
3,590
3,960
3,980
3,810
3,290
4,120
2,950
3,170
3,460
3,500
3,550
3,950
3,380
3,380
3,440
100
100
96
93
94
83
100
96
100
60
95
93
73
100
100
Oxygen
Transferred1
Ob per day)
33
450
467
480
529
494
562
583
625
591
580
562
556
517
503
BOD Removed
» Influent BOD/MLVSS
(Ib per day)
-------
&}-
,
BCC
T nr
linn :i:
ir
02
04
06
08
INFLUENT BOD5 IILVSS ( Ib/d/lb)
43
FIGURE 19
-------
Primary clarification efficiency had a measurable effect on the extended aeration basin
process loading versus BOD effluent quality. Prior to entering the aeration basin the VSS of
the clarified and blended wastewater varied from 300 to 410 pounds per day for the flows
measured. At these loadings the VSS averaged 0.1 pounds per pound of MLVSS. Without
primary clarification the ratio of VSS of the blended wastewater would be as high as 0.2
pounds per pound of MLVSS. As the ratio of blended influent VSS to MLVSS increased, a
poorer effluent quality for a given process loading resulted. This indicates the relative
importance of removing the inert volatile suspended matter from the waste prior to its
entering the aeration basin.
The design criteria for the aeration basin may be derived from the graph in Figure 19. For
example, an effluent BOD of 60 mg/1 will require an influent loading of 0.04 pounds of
BOD per pound of MLVSS.
In Arrangement No. 1, it was found that with the process loadings evaluated there was little
measurable difference in efficiency due to changes in NSSC wastewater percentages.
Removal of VSS in the primary clarifier provided improved effluent quality at the same
BOD to MLVSS loading.
Extended Aeration with Primary Clarification and Biofiltration - Arrangement No. 3
The aeration basin was operated with primary clarification of the raw NSSC waste and
biofiltration of the blended NSSC-domestic wastewater from October, 1971, to March,
1972. The percentage of NSSC wastewater loading ranged from 44 to 100 percent using
Arrangement No. 3. The hydraulic loadings to the biofilter were varied by changing the
recirculation ratio, and normally these rates exceeded 40 mgd/acre. In order to maintain
sufficient flow to rotate the trickling filter arm (at 100 percent NSSC wastewater) tap water
was added to the NSSC waste.
The performance of the extended aeration basin under different ratios of NSSC to domestic
wastewater is illustrated by Figure 20. The performance of this process is based upon results
summarized in Table 8. At the range of process loadings tested, it is seen that a poorer
quality effluent resulted with the 100 percent NSSC wastewater at a given loading. For
example, a process loading of 0.15 pounds of BOD per pound of MLVSS would result in an
effluent BOD of approximately 150 mg/1. On the other hand, the same process loading
(0.15 Ib BOD/lb MLVSS) would give an effluent BOD of 50 mg/1 in the case of a blended
NSSC-domestic waste.
The design criteria for the aeration basin under Arrangement No. 3 may be derived from the
graph in Figure 21. For example, an effluent BOD of 60 mg/1 will require an influent
loading of 0.001 pounds of BOD per pound of MLVSS for the 100 percent NSSC
wastewater and 0.16 pounds of BOD per pound of MLVSS for the blended NSSC and
domestic wastewater.
44
-------
300
270
240
.
0 3
0 4
0 5
0 7
INFLUENT BODK MLVSS (Ib d Ib)
45
FIGURE 20
-------
TABLES
EXTENDED AERATION RESULTS - (OCTOBER 13,1971 - MARCH 2,1972)
ARRANGEMENT NO. 3
Date
10/13/71
14
20
21
26
27
28
11/2/71
3
4
9
10
16
23
30
12/1/71
7
8
14
15
21
22
28
Operating
Teinpentur
(°C.)
23
25
26
26
24
24
26
25
23
20
16
17
21
16
16
17
18
18
19
21
19
17
17
e MLVSS
(matt
2,240
2,940
3,280
2,960
3,110
3,240
3,200
2,840
3,160
3,420
4,000
3,760
1,920
2,520
2,780
2,940
1,350
1,400
2,640
2,400
1,780
2,160
1,000
Percent NSSC
Watte Bued
on BOD
97
63
72
47
100
67
79
79
82
96
96
57
91
44
87
60
83
97
92
100
58
Oxygen
BODRetnorad
BOD
Tranrfened* Influent BOD/MLVSS Percent
Ob pet day)
-------
TABLE 8 (Continued)
EXTENDED AERATION RESULTS - (OCTOBER 13,1971 - MARCH 2,1972)
ARRANGEMENT NO. 3
Date
1/4/72
11
12
13
19
20
25
26
27
2/1/72
2
3
8
9
10
15
16
17
22
23
29
3/1/72
2
Operating
Temperature
16
18
17
19
16
17
IS
16
12
12
11
11
13
12
13
12
12
12
12
11
15
15
16
MLVSS
(mg/0
940
1,880
800
1,660
2,360
2,940
2,960
2,720
2,100
2,300
1,820
2,220
1,260
1,620
1,160
2,740
2,200
2,980
2,580
2,060
1,740
2,060
1,060
Percent NSSC
WuteBued
on BOO
73
52
100
100
79
100
100
67
99
54
56
89
90
72
83
64
61
98
61
85
75
100
66
Oxygen
Trmifened*
(ft per day)
235
-
177
315
222
-
-
_
-
-
-
-
-
-
-
-
-
-
-
_
BOD Removed
(tb per day)
544
201
108
292
260
104
71
60
109
119
109
165
87
86
55
92
122
65
93
92
134
41
135
(Ib/ingd)
-
-
-
1,736
780
-
-
1,337
-
608
-
-
-
689
-
-
-
486
-
Influent BOD/MLVSS
(Ib/day/lb)
0.837
0.286
0.412
0.313
0.227
0.140
0.037
0.031
0.063
0.061
0.074
0.092
0.099
0.093
0.117
0.043
0.068
0.028
0.047
0.064
0.097
0.028
0.142
BOD
Percent
Removed
69
37
33
56
49
24
65
72
82
85
81
81
69
57
41
77
82
77
76
70
79
72
89
Effluent
(mg/0
200
293
242
248
220
279
73
73
69
69
91
119
137
211
267
143
129
95
138
189
187
85
87
Excel*
Sludge
(Ib/mvO
_
_
_
280
1,724
-
_
4,198
3,336
__
_
_
8,388
_
_
-
6,505
Influent
VSS
(Ib/mjjd)
i_
-
997
1,668
_
1,750
-
166
-------
100
90
80
70
60
50
40
30
20
10
~-/r
/
t
.t.
-£-
7
f
f
'
'
0. 1
0.2 0.3 0.4 0.5
'NFLUENT BOD5 ACTUAL MLVSS (It) d ID)
48
0.6
0.7
FIGURE 21
-------
Extended Aeration with Biofiltration - Arrangement No. 4
The aeration basin was operated with biofiltration of the blended wastewater and
unclarified NSSC wastewaters during March, 1972. The percentage of NSSC wastewater
loading ranged from 50 percent to 100 percent using Arrangement No. 4. The effluent from
the biofilter was clarified in the intermediate clarifier.
Performance of the extended aeration process with biofiltration was based upon the results
summarized in Table 9. A comparison of BOD loading to effluent quality is shown in Figure
21. The graph shows no significant difference in effluent quality of the various percentages
of the NSSC wastewater evaluated.
The data in Table 9 does show a slightly lower MLVSS than in Arrangements No. 1 or 3.
This might, in part, be due to the lower VSS loading (approximately 75 pounds/day VSS) to
the aeration basin during Arrangement No. 4.
The design criteria for the aeration basin under Arrangement No. 4 may be derived from
Figure 21. For example, an effluent BOD of 60 mg/1 will require an influent loading of 0.29
pounds of BOD per pound of MLVSS for the blended domestic and unclarified NSSC
wastewaters.
Performance of Arrangements No. 1, No. 3 and No. 4
The relative performance of the extended aeration process following primary clarification,
biofiltration and both pretreatment processes, was evaluated. A comparison of the
arrangements indicated biofiltration provided the best effluent quality at the highest process
loading. The effluent BOD concentration of 60 mg/1 was used as a comparison figure which
corresponds to approximately 97 percent BOD removal. To achieve the desired end results
(60 mg/1 BOD) the process loadings would have to be adjusted for each arrangement as
shown below:
Process Loading Effluent BOD
Arrangement No. Description (Ib BOD/day/lb MLVSS) (mg/1)
1 Primary clarification 0.04 60
3 Primary clarification 0.001-0.16 60
plus biofiltration
4 Biofiltration 0.29 60
In the case of Arrangement No. 3, the lower limit of the loading range (0.001 Ib BOD/day/lb
MLVSS) provided an effluent of 60 mg/1 when the wastewater was 100 percent NSSC waste.
Temperature variations (11° 32° C.) were considered to have negligible effects on the
49
-------
en
O
TABLE 9
EXTENDED AERATION RESULTS - (MARCH 3-29,1972)
ARRANGEMENT NO. 4
Date
3/7/72
8
9
14
15
16
21
22
23
28
29
Opmting FwcmtNSSC
Tempentue MLVSS WMto fined
f°CJ (raft on BOD
14
14
13
16
17
18
18
17
15
18
19
1,100
1,380
1,580
620
2,100
1,900
1,860
1,080
1,960
1,640
2,200
60
95
100
86
66
78
85*
77
62
75
100
Oxygen BODR«norad
Tnarfened* I
Obpwdey) Obpef day) Ob/m*0
320
314
278
332
209
201
119
316
275 324
299 318
331 327
2^49
2,256
1,356
-
-
-
2,490
-
W13
BOD
nfhMUtBOD/MLVBS Percent Effluent
CIWdty/lb) Renored (mart)
0.341
0.271
0.219
0^39
0.125
0.134
0.087
0311
0.181
0.211
0.171
85
84
80
84
80
79
74
94
91
92
87
45
60
66
49
41
41
40
18
28
26
46
Excew
ShidfB
Ob/mid)
2,565
1,916
-
9^65
7,725
-
4,512
Inflnent
VSS
OWnwO
mm
747
170
-
169
85
254
Stsndud condtttoni, 5.5 percent tnmfet effldeocy
-------
aeration process since the BOD loading was maintained well below 0.5 pounds of BOD per
pound of MLVSS per day. At higher loadings temperature jwould have a noticeable influence
on the aeration basin effluent quality.
Extended Aeration Oxygen Requirements and Utilization
The oxygenation characteristics of the combined NSSC waste and domestic wastewater vary
with the percentage of NSSC waste based on BOD. These oxygenation characteristics were
determined for the combined waste with 20 percent and 75 percent NSSC waste.
Alpha (a)
The alpha (a) coefficient was determined for several different percentages of NSSC and
domestic wastewater utilizing diffused aeration. The aeration rate was maintained constant
for tap water aeration and waste aeration for each "a" value determined.
The alpha (a) values were calculated from the following mathematical derivation:
W = <|c = KLa (C* - C)
dt
Where C = dissolved oxygen concentration at time t
C* = equilibrium dissolved oxygen concentration
t = time
W = weight of water
KLH = overall mass transfer coefficient
The integration of the above equation yields
_ /2.303 W\ / log <
^La
where subscripts 1 and 2 refer to measurements at times 1 and 2, respectively.
Since the sample volume was identical for both the tap water and the waste samples, these
expressions of KLa may be simplified to
51
-------
The above equation may be solved graphically by plotting (C* - C) versus time on
semi-logarithmic paper and determining the time interval for one cycle.
thence
(waste)
. . , ,
alpha (a) =
(tap water)
tap water
The oxygenation data was evaluated and alpha (a) values for various percentages of NSSC
wastes were determined. Table 10 correlates the alpha (a) values determined versus the
NSSC percentage of that waste. Figure 22 shows the correlation of alpha (a) versus various
NSSC percentages of the combined waste.
Beta(0)
The beta (0) factor expresses the ratio of the saturation of dissolved oxygen in a waste to
saturation in tap water at given conditions.
The saturation of oxygen in combined NSSC-domestic wastewater was found to vary with
the percentage of NSSC waste. The correlation of beta (0) to the percentage of NSSC waste
is shown in Table 10 and in Figure 22. Figure 22 shows that for several percentages of NSSC
waste evaluated, both alpha and beta decreased with increasing NSSC percentages of the
wastewater.
Oxygen Utilization
The air applied, temperature and dissolved oxygen of the mixed liquor in the aeration basin
were monitored daily. These data, as well as the alpha (a) and beta (0) values, were utilized
to evaluate the oxygen requirements of the extended aeration process. All data were
corrected to standard conditions for interpretation. The oxygenation data, given in Table
11, were adjusted to an arbitrary MLVSS concentration of 3,000 mg/1 to permit correlation
of the data. The oxygen applied relative to BOD removed data is shown graphically in
Figure 23. The curve of best fit for these data indicates the following oxygen requirement at
standard conditions:
Oxygen requirement = 0.97 BOD removed + 0.07 MLVSS
52
-------
TABLE 10
ALPHA (a) AND BETA (0)
VS. PERCENTAGE NSSC WASTE
Date
Percentage NSSC Waste
Based on Flow
L
Temperature
9/22/71
9/23/71
10/13/71
10/14/71
76
72
18
21
0.42
0.57
0.88
0.65
0.77
0.42
0.93
0.87
29
31
31
23
53
-------
60
0 2
0 4
0 6
0 8
1 0
1 2
ALPHA (O) AND BETA (j3) VALUES
54
FIGURE 22
-------
TABLE 11
O2 APPLIED VS. BOD REMOVED*
Oxygen Applied
Date (Ib per day)
7/20/71
21
22
27
28
29
8/10/71
11
12
17
18
19
24
25
26
10/13/71
14
20
21
26
27
28
17
193
199
199
254
189
301
290
306
286
277
224
259
259
248
460
289
316
367
354
336
334
BOD Removed Oxygen Applied
(Ib oer dav) Date (Ib per day)
61
71
58
73
68
64
91
65
41
69
44
54
57
34
42
309
214
169
200
228
277
210
11/2/71
3
4
9
10
16
23
12/1/71
7
8
14
15
21
22
1/11/72
13
19
20
3/23/72
28
29
376
423
495
421
371
688
670
656
766
746
417
417
711
609
432
344
533
281
601
632
485
BOD Removed
(Ib per day)
105
221
170
221
238
113
208
402
157
123
225
325
184
244
109
150
154
82
148
151
223
*Data corrected to standard conditions and 3,000 mg/l MLVSS
55
-------
56
FIGURE 23
-------
Additionally, the actual oxygen utilization in the aeration basin was measured on several
occasions in a BOD bottle with a Yellow Springs dissolved oxygen probe. These data, given
in Table 12, were adjusted to an arbitrary MLVSS concentration of 3,000 mg/1 and standard
condition, as shown in Table 13. These data were compared graphically to BOD removed as
shown in Figure 24. The oxygen utilization curve from Figure 23 was superimposed on
Figure 24. This superimposition showed the oxygen requirements determined by the two
different methods to be very similar.
The oxygen requirements design criteria for the aeration basin can be taken from Figure 23.
For example, 600 pounds of oxygen per day would be required to remove 400 pounds of
BOD per day.
In summary, design criteria for oxygen requirements were determined by oxygenation
studies. These included alpha (a) and beta (0) determinations for various percentages of
NSSC wastes. They also included correlations of oxygen applied versus BOD removed.
Waste Sludge
The excess sludge from the activated sludge facility was estimated by making a material
balance on the system. The excess sludge was adjusted to an arbitrary flow (1.0 mgd) and an
effluent VSS concentration of 35 mg/1. The quantities of excess sludge were compared to
BOD removed (Figure 25) and influent VSS (Figure 26). The wide distribution of data
shown in Figures 25 and 26 would not permit a correlation to be made between the BOD
removed or the influent VSS. As a result, the quantities of excess sludge could not be
estimated from the data collected.
Cellulose fibers are difficult to degrade aerobically and the quantities of excess sludge can be
conservatively estimated as:
Excess sludge = Influent suspended solids + 0.47 (BOD) removed - Effluent suspended solids
This expression does not reflect the VSS loss due to endogenous respiration. The inert VSS
(cellulose fiber) in the raw settled NSSC waste will not permit the theoretical endogenous
respiration constant to be applied to MLVSS.
In summary, no definite conclusion could be reached as to the amount of excess sludge
produced from normal operation of the extended aeration process.
The major findings from the extended aeration pilot plant studies are as follows:
1. There were no appreciable performance differences due to
changes in the percentage of NSSC wastewater. VSS removal
of blended influent improved the quality of the effluent at a
given unit process loading.
57
-------
I/I
00
TABLE 12
O2 UPTAKE
AERATION BASIN DATA
9/21/71
Time
(m3nl
0
0.5
1.0
1.5
2.0
2.5
3.0
3.5
DO
(ma/1)
9
4.5
1.7
0.7
0.3
0.2
0.1
0
_
9/21/71
Time
(min)
0
0.5
1.0
1.5
2.0
2.5
DO
(mi/I)
9.0
5.5
2.0
0.6
0.1
0
9/22/71
Time
(min)
0
0.5
1.0
1.5
2.0
2.5
3.0
3.5
4.0
4.5
5.0
5.5
6.0
DO
9.4
6.7
4.5
2.7
1.3
1.0
0.6
0.4
0.3
0.2
0.2
0.1
0.1
10/14/71
Time.
(min)
0
0.5
1.0
1.5
2.0
2.5
3.0
3.5
4,0
4.5
_
__
H«_
DO
4.7
2.7
1.8
1.3
1.0
0.8
0.6
0.5
0.2
0
_
_
_
10/14/71
Time
(min)
0
0.5
1.0
1.5
2.0
2.5
3.0
3.5
4.0
_
_
_
DO
6.1
2.9
1.9
1.5
1.1
0.8
0.5
0.1
0
_
-------
TABLETS
O2 UPTAKE VS. BOD REMOVED*
Date
9/21/71
9/21/71
9/22/71
10/14/71
10/14/71
O2 Uptake x MLVSS (mg/1)
94
281
134
814
1,178
BOD Removed
32
32
211
356
369
(mg/1)
*Data corrected to standard conditions and 3,000 mg/1 MLVSS
59
-------
3.000
2.000
1 . 000
01
u.
100
200
300
400
500
BOD5 REMOVED (Its d)
60
FIGURE 24
-------
4 000
3 500
3 000
2 500
!
2 000
I 500
1.000
500
__
LJ
2 000
4 000 6.000 8 000
A SLUDGE OPTIMUM CONDITIONS ( Ibs mgd)
'
12.000
14, 000
FIGURE 25
-------
8. 000
7. 000
6. 000
5.000
4 000
3.000
2 000
1 . 000
2 000 4 000 6.000 8.000 10 000
SLUDGE OPTIMUM CONDITIONS (IBs mgd)
62
FIGURE 26
-------
2. Of the three arrangements tested, biofiltration provided the
greatest single improvement in effluent quality of the
aeration basin at a given process loading.
3. Alpha and Beta values depended greatly upon the percentage
of NSSC wastewater present, and the values ranged from 0.42
to 0.88 and 0.42 to 0.93, respectively.
4. Oxygen requirements were determined to be 0.97 pounds per
pound of BOD removed plus 0.07 pounds of oxygen per
pound of MLVSS in the aeration basin.
63
-------
SECTION X
FINAL CLARIFICATION
The separation of the activated sludge from the aeration basin effluent was accomplished
with a clarifier with sludge rakes and a hopper bottom. The clarifier was operated for the
duration of the study-May, 1971, through April, 1972. The unit was evaluated according to
its operating performance at various overflow rates, water temperatures and wastewater
composition.
Operation
The effective size of the final clarifier was 15 feet in diameter with a sidewater depth of
12.9 feet. The unit was operated at different flows to provide variations in overflow rates,
detention times and solids loading. Data was compiled based upon grab samples collected at
sampling locations as shown in Figure 2, and these included the aeration basin effluent, the
clarifier underflow and the final clarifier effluent.
Over the period of operation the activated treatment system encountered different food to
microorganism ratios, temperatures, industrial wastewater concentrations and other
conditions which influenced its performance. These factors also had some effect on
consistent performance of the final clarifier.
Performance
The results of monthly average performance data on the final clarifier are shown in Table
14. It can be seen that a very high suspended solids removal of 95 percent was achieved over
the study period. In addition, BOD removal was 85 percent. Figure 27 gives the relationship
between the BOD and the total suspended solids removed.
Design considerations are shown in Figure 28. From this figure, it can be seen that increases
in detention time and decreases in overflow rate bring about reductions in the percentage
removal of total suspended solids. It is also shown that lower temperatures reduce the
performance of the clarifier, i.e., 95 percent removal requires an overflow rate of
approximately 1,200 gpd/sq ft at 61° F., where almost 1,500 gpd/sq ft at 82° F. gives the
same performance. The temperatures of the wastewater should be considered when the final
clarifier is designed.
In the range of NSSC waste to domestic wastewater flows tested, no significant effects on
final clarification were noted. At the low loadings of the extended aeration basin it is
believed that settling was enhanced considerably. At higher food to microorganism ratios
the settling in the final clarifier would be hampered.
64
-------
TABLE 14
FINAL CLARIFIER PERFORMANCE
(MONTHLY AVERAGE DATA)
Month
June
July
August
September
October
November
December
January
February
March
Flow w/recirc.
(1,000 gpd)
146
117
168
112
217
210
238
224
167
1%
Overflow
Rate
(gpd/«q ft)
826
662
950
634
1,228
1,188
1,347
1,268
945
1,109
Water
Temperature
79
82
84
86
77
66
64
59
54
61
NSSC Waste
{% Raw Flow)
10
15
17
42
18
16
19
22
24
14
Inlet
TSS
(lb per day)
2,989
4,491
5,678
6,615
6,210
5,657
4,254
4,196
3,242
2,975
Inlet
BOD
(lb per day)
626
579
660
1,185
1,242
1,762
2,062
1,431
1,348
1,353
Removal by Sedimentation Det
TSS BOD Time
(percent) (percent) (min)
93
97
98
99
94
96
91
95
93
94
64
70
87
74
92
97
92
85
91
96
174
216
150
228
120
120
108
114
150
130
Solids
Loading
(lb/sq fyday)
17
25
32
37
35
32
24
24
18
17
Avenge
180
1,019
71
19
4,631
1,225
95
85
151
26
-------
10 000
9 000
8 000
7.000
E 000
5 000
4 000
3 000
2 000
1.000
/
I
'-I-
11
It
]Q]
IRC
IE
in v
lit
1*1
FrnrBJSiarnH-iMnip-
vrtt
500
t 000 1 500 2.000
B005 REMOVED (Ib day)
66
2 500
3.000 3,500
FIGURE 27
-------
240-1
1.500
200 -
1. 250-
160 -
1.000-
120 -
750-
80-
500
40 -
250-
0 -1
100
TSS REMOVED (PERCENT )
FIGURE 28
-------
SECTION XI
COLOR REMOVAL
Paper mill wastewaters are noted for their color problems. The raw wastewater from the
neutral sulfite semichemical pulp and paper waste has a deep brown-black color. Chemical
precipitation with lime as a coagulant at various pH levels has been the most widely
accepted method of color control. However, massive dosages of lime often are required to
produce adequate reductions in color and the process may involve several steps. As a result,
the process requires recalcining of the lime and is usually very expensive.
Laboratory studies were conducted on various ratios of NSSC and domestic wastewater
using massive lime dosage followed by chlorination. The test procedures and findings are
discussed in depth but the economics of this type of treatment were not investigated in
detail.
Test Procedure
The color removal studies were conducted using a jar test procedure. The wastewater
samples which were studied were composed of NSSC waste, and one part NSSC waste to
one part domestic wastewater. In the precipitation studies only hydrated lime was used,
which is native to the Harriman area. The chlorine source for the chlorination studies was
calcium hypochlorite.
The jar test procedure consisted of dosing batch samples of the wastewater with known
quantities of lime. The wastewater and lime were mixed rapidly for IS seconds, flocculated
slowly for 15 minutes and allowed to settle. The supernatant was chlorinated after the pH
was adjusted to neutrality and the color determination was made. After chlorinating, the
color was again measured by a colorimeter at a pH of 7.
Findings
Findings from the color removal studies are reported in Table 15. These studies include the
massive lime treatment and chlorination. The results of the analyses on different mixes of
NSSC and domestic wastewater are given in Figures 29-32. In Figure 29, it can be seen that
increased dosages of lime on the NSSC waste reduced the APHA color significantly. The
lowest color achieved was approximately 7,500 APHA units at 32,000 mg/1 of lime. In the
case of the one to one wastewater mixture, a dosage of slightly more than 22,000 mg/1 gave
the best color quality (Figure 30).
68
-------
TABLE 15
RESULTS OF COLOR REMOVAL STUDIES
CaO
Dosage
(mg/l)
0
7,570
7,570
7,570
7,570
7,570
7,570
15,140
15,140
15,140
15,140
15,140
15,140
22,710
22,710
22,710
22,710
22,710
22,710
30,280
30,280
30,280
30,280
30,280
30,280
37,850
37,850
37,850
37,850
37,850
37,850
Chlorine
Dosage
(mg/l)
0
0
0
800
600
400
200
0
0
800
600
400
200
0
0
800
600
400
200
0
0
800
600
400
200
0
0
800
600
400
200
PH
(After Treatment)
100 Percent NSSC Wastes
11.5
7.0
7.0
7.0
7.0
7.0
11.8
7.0
7.0
7.0
7.0
7.0
11.85
7.0
7.0
7.0
7.0
7.0
12.0
7.0
7.0
7.0
7.0
7.0
12.05
7.0
7.0
7.0
7.0
7.0
Color
at pH 7.0
(APHA Units)
24,250
22,850
17,160
10,350
12,800
14,750
15,850
14,200
12,950
5,940
7,550
10,100
11,275
10,250
9,550
3,900
5,650
8,070
9,100
8,100
7,820
2,015
4,060
6,435
8,110
7,650
8,100
4,350
4,900
5,700
7,500
69
-------
TABLE 15 (Continued)
RESULTS OF COLOR REMOVAL STUDIES
CaO
Dosage
(mg/l)
Chlorine
Dosage
PH
(After Treatment)
Color
at pH 7.0
(APHA Units)
50 Percent NSSC Waste-50 Percent Domestic Wastewater
5,680
5,680
5,680
5,680
5,680
0
7,570
7,570
7,570
7,570
7,570
7,570
7,570
7,570
7,570
7,570
7,570
11,355
11,355
11,355
11,355
11355
15,140
15,140
15,140
15,140
15,140
15,140
1,000
800
600
400
200
0
0
0
1,000
800
800
600
600
400
400
200
200
1,000
800
600
400
200
0
0
800
600
400
200
7.0
7.0
7.0
7.0
7.0
6.6
12.2
7.0
6.9
7.0
7.0
7.0
6.9
7.0
6.9
7.0
6.9
7.0
7.0
7.0
7.0
7.0
12.4
7.0
7.0
7.0
7.0
7.0
1,440
1,720
2,800
5,275
6,500
12,200
7,360
4,290
1,120
1,130
925
1,180
1,815
2,640
3,900
3,960
4,950
950
1,015
1,150
2,880
4,200
6,250
3,060
650
672
1,140
2,930
70
-------
TABLE 15 (Continued)
RESULTS OF COLOR REMOVAL STUDIES
Ca O Chlorine Color
Dosage Dosage pH at pH 7.0
(mg/l) (mg/l) (After Treatment) (APHA Units)
50 Percent NSSC Waste-50 Percent Domestic Wastewater
22,710 0 12.5 5,320
22,710 0 7.0 2,665
22,710 2,000 7.0 189
22,710 1,000 7.0 277
22,710 800 7.0 630
22,710 800 12.5 378
22,710 800 7.0 650
22,710 600 7.0 638
22,710 600 7.0 468
22,710 600 7.0 650
22,710 400 7.0 830
22,710 400 7.0 780
22,710 200 7.0 2,600
22,710 200 7.0 2,210
45,420 1,000 8.5 136
45,420 800 8.5 176
45,420 600 8.5 240
45,420 400 8.5 488
45,420 200 8.5 1,440
15 Percent NSSC Waste-85 Percent Domestic Wastewater
00 - 3,750
757 0 9.7 5,150
3,785 0 10.9 1,470
5,678 0 - 1,160
7,570 0 10.6 1,130
11,355 0 - 920
71
-------
FIGURE 29
-------
8. 000
7 000
6 000
la
t-
z
: 5 000
c
QB
0
-1
U
4 000
3 000
2 000
000
0
\
\
\
V
\
\
\
\
x
s
">
X
X
-,
^^
1
s^^
^^
^.
>-
-~
«s
=;.
A
I
D
cc
1_(
ntrw
Msic
iR
1
R
"
UtP
K
I
«vN
u\
'
c
AT f
VA^SI
'AP1ER
N
L
w
rK i E
STtW
LL{W
AS
E;
10 000 20 000 30 000
Cat) DOSAGE (mg 1 )
73
FIGURE 30
-------
20.000
18 000
16.000
14 000
12 000
1 0 000
8.000
6 000
4 000
s
71
la )
(I
( aO
2.0 00
C 3LJOR HEUIOVALAND
LIME
C -ILOF INE
NSSfc
/ASTE
3CMESTIC
WAST
200
400
600
CHLORINE (mg I)
74
FIGURE 31
-------
CHLORINE DOSAGE (mg I) AT pH 7 0
COLOR REMOVAL AND LIME + CHLORINE:
50% NSSC + 50* WASTEWATER
TREATMENT OF DOMESTIC WASTEWATER
AND NSSC PULP AND PAPER MILL WASTES
FIGURE 32
-------
Chlorination of the NSSC wastewater after massive lime treatment reduced its color to as
low as 2,000 APHA units. This is shown in Figure 31. A similar reduction is shown by
Figure 32 where the NSSC wastewater diluted with domestic wastewater was reduced to
100 APHA units. In this case, increased chlorination did not bring about further reductions
in color for chlorine dosages above 800 mg/1.
Overall, the lime treatment was very effective and chlorination reduced the color further.
However, based upon the laboratory results, the dosages of lime would be as high as 45,420
mg/1 or up to 190 tons per million gallons of wastewater to be treated. This would require
investigation of a lime reuse process, such as recalcining, in order to determine the economic
feasibility of color removal by this method. Chlorination would appear to be a relatively
small proportion of the total chemical cost of color removal.
76
-------
SECTION xn
DISINFECTION
Disinfection studies on the treated NSSC and domestic wastewater using chlorine and
chloramines were conducted in the laboratory from November, 1971, through March, 1972.
Procedure
Total and fecal coliform analyses using the membrane filter method, as described in the
13th edition of Standard Methods for the Examination of Water and Wastewater, were run
at the pilot plant site to evaluate effluent disinfection.
The waste entering and leaving the chlorine contact chamber with no chemicals added was
analyzed for total and fecal coliform for one month to establish a baseline for future
comparison. Then laboratory studies on the effect of chlorine and combination of chlorine
and ammonia application, application sequence and contact time on disinfection were made.
The contact time included both the mixing time between the addition of the first and
second chemical, and the mixing time of the combined chemicals and the waste.
The mixing time between the addition of the first and second chemical was varied from 3 to
45 minutes. The mixing time of the combined chemicals and the waste was varied from 5 to
78 minutes. Chlorine followed by ammonia and ammonia followed by chlorine application
sequences were evaluated. Chlorine and ammonia application ranged from 1040 mg/1 and
0 40 mg/1, respectively.
Results
The results of the disinfection studies are shown in Tables 16 through 21. Table 16 shows
the baseline total and fecal coliform determinations. The effects of varying the application
and the application sequence are shown in Tables 17-20. The effects on the effluent of
adding chlorine alone are shown in Tables 20 and 21. The effects of varying the contact
time are shown in Tables 18 and 19.
The contact time studies were run concurrently with application and sequence studies.
Recommended contact times of 5 minutes for the mixing of the waste and ammonia and 15
minutes for the mixing of the combined waste and chemicals after chlorine is added were
reached by choosing those minimal times which resulted in consistent 100 percent coliform
removal. Contact time evaluations were hindered by the fact that other parameters were also
varied during that period.
77
-------
TABLE 16
DISINFECTION STUDIES
COLIFORM BASELINE DETERMINATION
00
Influent Pint Chemical Contact Time Second Chemical
Cottfotm Added Concentration Pint Chemical Added Concentration
Count (MPN) (mg/0 andWaite (mgft
Date
10/7/71
10/8/71
10/11/71
10/12/71
10/13/71
10/18/71
10/19/71
10/20/71
10/27/71
Total
28,000
160,000
40,000
24,000
100,000
240,000
36,000
23,000
35,000
Fecal NH3 Cl (mfa) NHj a
No Chemical* Added
120,000
33,000
26,000
18,000
2,000
5,000
11,000
1,000
Contact Time Colifarin Removal
Both Chemfcalf Effluent CoUfoon Efficiency
and Watte Count (MPN) (percent)
(mm) Total
30,000
120,000
28,000
24,000
70,000
240,000
11,000
23,000 .
31,000
Fecal Total Fecal
_
_
- - -
_
_ _
_ _
_ _ -
_ _ _
-------
TABLE 17
DISINFECTION STUDIES
APPLICATION AND SEQUENCE EVALUATION
-j
vo
Influent Pint Chemical
Cotifotm Added Concentration
Count (MPN) (mg/0
Date
11/1/71
11/2/71
11/3/71
11/8/71
11/9/71
11/10/71
11/15/71
11/16/71
11/17/71
11/22/71
11/23/71
11/27/71
11/29/71
11/30/71
Total
10,000
38,000
4,000
12,000
4,000
7,000
14,000
12,000
12,000
2,000
16,000
15,000
20,000
6,000
Fecal
12,000
N.D.
56,000
18,000
1,000
800
2,700
30,000
6,000
17,000
29,000
16,000
10,000
7,000
NH3
40
20
40
-
-
-
20
15
-
-
-
8
10
Cl
35
-
-
-
40
30
15
-
-
10
15
15
-
Contact Time
Pint Chemical
and Waste
(min)
3
3
3
3
3
3
3
3
3
3
3
3
3
3
Second Chemical
Added Concentration
(mg/D
NH3
0
-
-
_
0
0
0
-
-
0
0
0
-
a
35
18
20
40
30
15
15
15
10
15
15
15
15
Contact Time
Both Chemicals
and Waste
(min)
68
68
68
72
72
72
78
78
78
46
40
37
41
41
Effluent Collforni
Count (MPN)
Total
5,000
100
400
200
N.D.
700
28,000
3,000
N.D.
5,000
8,000
6,000
10,000
N.D,
Fecal
2,300
N.D,
42,000
N.D,
N.D.
200
140,000
N.D.
N.D,
14,000
16,000
8,000
5,000
N.D.
CoUfoim Removal
Efficiency
(percent)
Total
50
99
90
99
100
90
_
75
100
-
50
60
50
100
Fecal
81
_
100
100
100
75
t
100
100
18
45
50
50
100
N.D. - None Detected
-------
TABLE 18
DISINFECTION STUDIES
APPLICATION, SEQUENCE, AND CONTACT TIME EVALUATION
00
o
Influent Pint Chemical
CoUform Added Concentration
Count (MPN)
Date
12/1/71
12/6/71
12/7/71
12/8/71
12/13/71
12/14/71
12/15/71
12/20/71
12/21/71
12/27/71
12/28/71
Total
12,000
42,000
12,000
13,000
23,000
8,000
5,000
14,000
6,000
11,000
24,000
Fecal
10,000
54,000
40,000
32,000
10,000
4,000
3,000
N.D.
NJX
N.D.
10,000
(mg/l)
NH3
15
-
-
40
-
-
40
30
30
20
20
a
20
20
20
20
-
-
-
-
Contact Time
Pint Chemical
and Waste
(min)
3
3
3
5
5
5
5
5
15
5
20
Second Chemical
Added Concentration
(mgfl)
NH3
20
30
_
40
40
-
-
-
-
a
15
-
-
20
-
-
20
15
15
10
10
Contact Time
Both Chemicab
and Watte
(min)
39
39
55
50
43
41
40
41
44
47
42
Effluent CoUform
Count (MPN)
Total
3,000
26,000
13,000
N.D.
3,000
7,000
15,000
11,000
14,000
6,000
3,000
Fecal
10,000
50,000
27,000
N.D.
N.D.
N;D.
N.D.
N.D.
N.D.
N.D.
N.D.
CoUform Removal
Efficiency
(percent)
Total
75
38
-
100
87
125
-
21
-
45
88
Fecal
N.D.
7
3
100
100
100
100
-
-
-
100
N.D. - None Detected
-------
TABLE 19
DISINFECTION STUDIES
APPLICATION, SEQUENCE, AND CONTACT TIME EVALUATION
oo
Influent Pint Chemical
Colifonn Added Concentration
Count (MPN) (mg/1)
Date
1/3/72
1/4/72
1/5/72
1/10/72
1/11/72
1/12/72
1/17/72
1/18/72
1/19/72
1/24/72
1/25/72
1/26/72
1/31/72
2/1/72
2/2/72
Total
11,000
11,000
20,000
26,000
9,000
27,000
4,000
22,000
40,000
9,000
31,000
6,000
13,000
19,000
4,000
Fecal
20,000
8,000
11,000
1,000
6,000
9,000
1,000
7,000
3,000
N.D.
1,000
1,000
N.D.
2,000
N.D.
NH3 a
40
40
40
40
40
40
40
40
40
20
40
40
40
40
40
Contact Time
Pint Chemical
and Waste
(min)
20
30
45
45
45
45
45
45
45
45
45
45
30
15
15
Second Chemkal
Added Concentration
(mg/l)
NH3 a
20
20
20
20
20
20
20
20
20
40
20
20
20
20
15
Contact Time
Both Chemicab
and Watte
(min)
43
43
43
5
15
15
15
15
15
15
15
15
15
50
51
Effluent CoUfonn
Count (MPN)
Total
N.D.
N.D,
N.D.
6,000
N.D.
N.D.
N.D.
1,000
N.D.
15,000
1,000
300
N.D.
2,800
1,400
Fecal
N.D.
N.D.
N.D.
N.D.
N.D.
N.D.
N.D.
N.D.
N.D.
400
N.D.
N.D.
N.D.
N.D.
N.D.
CoUfonn Removal
Efficiency
(percent)
Total
100
100
100
77
100
100
100
95
100
«.
97
95
100
85
65
Fecal
100
100
100
100
100
100
100
100
100
_
100
100
_.
100
N.D. - None Detected
-------
TABLE 20
DISINFECTION STUDIES
EFFLUENT COLIFORM AFTER CHLORINATION
oo
to
Date
2/7/72
2/8/72
2/9/72
2/14/72
2/15/72
2/16/72
2/21/72
2/22/72
2/23/72
2/28/72
2/29/72
Influent Pint Chemical
Colifom Added Concentration
Count (MPN) (mg/1)
Total Fecal NH3 d
- - - 10
- - 10
- - 10
10
- - - 10
- - 10
- - 10
- - - 10
- - - 10
- - 10
10
Contact Time Second Chemical Contact Time
Pint Chemical Added Concentration Both Chemical*
and Waste (mg/0 andWute
(min) NH3 Cl (min)
15 -
15 - -
15 - -
15 - -
15 - -
15 - -
15 - -
15 - -
15 - -
15 -
15 - -
Effluent CoUform
Count (MPN)
Total
32,000
20,000
59,000
19,000
17,000
15,000
20,000
6,000
4,000
8,000
9,000
Fecal
N.D.
N.D.
14,000
N.D.
1,000
N.D.
1,000
1,000
N.D.
2,000
N.D.
CoUform Removal
Efficiency
(percent)
Total Fecal
_ -
- -
- -
_ -
- -
-
N.D. - None Detected
-------
TABLE 21
DISINFECTION STUDIES
EFFLUENT COLIFORM AFTER CHLORINATION
oo
Date
3/1/72
3/6/72
3/7/72
3/8/72
3/12/72
3/13/72
3/14/72
3/20/72
3/21/72
3/22/72
3/27/72
3/28/72
3/29/72
Influent Fiat Chemical
Cottform Added Concentration
Count (MPN) (mj/0
Total Fecal NH3 Cl
- 10
- ~ 10
10
- - 10
- - 10
- - 10
- _io
_ 10
- 10
_ - 10
- - - 10
- 10
- 10
Contact Time Second Chemical Contact Time
Pint Chemical Added Concentration Both Chemicals
and Watte (mtf 0 and Waste
(mln) NH3 Cl (min)
15 -
15 -
15 -
15 -
15 -
15 - -
15 -
15 -
15 - -
15 -
15 - -
15 -
15 - -
Effluent CoUform
Count (MPN)
Total
2,000
40,000
50,000
4,000
20,000
24,000
7,000
6,000
4,000
60,000
50,000
500
30,000
Fecal
2,000
28,000
1,000
2,000
35,000
68,000
N.D.
2,500
300
4,000
8,300
1,100
1,900
Conform Removal
Efficiency
(percent)
Total Fecal
_
_
_ _
c
_
- -
- -
_ _
- -
N.D. - None Detected
-------
An example comparing the application sequences from Tables 17-20 with concentration
of ammonia and chlorine held constant is shown below:
Date Application Sequence Total Fecal
12/13/71
12/14/71
1/3/72
1/4/72
Chlorine followed by ammonia
Chlorine followed by ammonia
Ammonia followed by chlorine
Ammonia followed by chlorine
87
125
100
100
100
100
100
100
This data shows that the ammonia followed by chlorine application sequence was more
effective in disinfection.
The amount of chlorine necessary to achieve 100 percent coliform removal is 40 mg/1 as
shown in Table 17, on November 9, 1971. The amount of ammonia plus chlorine necessary
to achieve 100 percent coliform removal is 40 mg/1 ammonia plus 20 mg/1 chlorine as shown
in Table 19 on January 3 and 4, 1972. According to current market prices for chlorine and
ammonia, the combination of ammonia and chlorine is less expensive than the higher
amount of chlorine. Thus, the combination of chlorine and ammonia should be more
economical.
In conclusion, the disinfection studies showed that the following procedure is the most
effective and economical in removing total and fecal coliform organisms:
1. Add ammonia at 40 mg/1 and allow at least a 5-minute
contact time.
2. After the 5-minute contact time, chlorinate at a
concentration of 20 mg/1.
3. Allow at least a 15-minute contact time.
4. Discharge as effluent.
84
-------
SECTION xm
DESIGN CONSIDERATIONS
In the following subsections the design considerations are summarized and reviewed from an
individual process and total treatment system standpoint. Emphasis was placed upon
performance, maintenance, design factors, and other items which were believed to be of
particular importance as a result of this pilot plant study. The processes covered included
primary clarification, biofiltration, extended aeration, final clarification and disinfection.
Primary Clarification of NSSC Wastewater
Due to the high cellulose concentration in the raw NSSC wastewater the VSS were
correspondingly high. Difficulty in removing the cellulose as VSS was one of the most
significant factors in primary clarifier design.
Overflow rates from 200 to 300 gpd/sq ft resulted in average suspended solids removal
efficiencies from 45 to 76 percent. Constant plugging by solids in piping and valves made
sludge drawoff difficult and resulted in lower suspended solids removal efficiencies. Only
minimal BOD and COD removals were achieved in the primary clarifier and these removals
were almost independent of the suspended solids removal.
Biofiltration
The performance of unit processes within the pilot plant treatment system was strongly
influenced by the high rate biofilter.
From a design viewpoint, the biofilter influent BOD and COD were reduced an average of
only 13 to 16 percent with biofilter loadings averaging 260 to 290 pounds of BOD per day
per thousand cubic feet of filter media. Primary clarification of the NSSC wastewater
improved the biofilter BOD removal performance by approximately 100 percent. Increased
proportions of NSSC wastewater reduced the performance of the filter to almost zero.
However, comparison of operating results of the extended aeration basin with and without
the biofilter markedly changed the extended aeration design requirements. Design
consideration for the biofilter should be based on the effect it has on the performance of
the extended aeration process and not on the reductions in BOD.
Extended Aeration
It was concluded in Section IX of this report that optimal extended aeration efficiency
occurred when the raw NSSC waste was clarified .and the combined NSSC-domestic
wastewater was treated by biofiltration.
85
-------
The process loadings, i.e., pounds of BOD per pound of MLVSS per day, should be less than
0.2 to obtain desirable effluent quality. Also, as long as this loading is maintained, the
temperature will have little effect on the removal efficiency of the aeration basin.
The nutrients in the combined NSSC-domestic wastewater were sufficient to maintain
biological activity in the aeration basin.
A range of 200 to 10,000 pounds of excess sludge was produced when 500 to 3,500 pounds
of BOD were removed per day. This depended largely on the aeration basin influent VSS of
the NSSC waste. Variations in the recirculation ratio of 5 to 75 percent did not affect
significantly the aeration basin efficiency.
Oxygen requirements for the extended aeration basin can be taken from Figure 23 where it
is shown that approximately two to three pounds of oxygen are required to remove one
pound of BOD in the aeration basin. This relatively high oxygen demand was probably
caused in part by the high oxygen demand of the sulfites in the NSSC waste.
Final Clarification
The effects of several operating conditions on solids settling were demonstrated.
The following operating parameters were maintained:
Operating Parameters Range of Values
Overflow Rate 600 to 1,300 gpd/sq ft
Process Loading 0.1 to 0.2 Ib BOD/lb MLVSS/day
Detention Time 1.5 to 4 hours
Temperature 54° to 86° F.
As a result, the final clarifier operated at a 91 to 99 percent TSS removal efficiency and 64
to 97 percent BOD removal.
Disinfection
The best disinfection results were achieved through the addition of 40 mg/1 ammonia and 20
mg/1 chlorine. The contact time after the addition of ammonia was at least 5 minutes. After
the addition of chlorine, the contact time was 15 minutes prior to discharge.
86
-------
SECTION XIV
ACKNOWLEDGMENTS
Mr. Stanley D. Kelley, Manager of the Harriman Utility Board, is acknowledged for his
support throughout the project. Mr. Amos G. Stuehser, Superintendent of Water and Sewer
Systems, Harriman Utility Board, was Project Director. Mr. Stuehser and associates are
acknowledged for analytical work and operation of the pilot plant.
The pilot plant faculty was designed by Black, Crow and Eidsness, Inc., Consulting
Engineers, under the guidance of Dr. James B. Goodson and Mr. Robert E. Rader. Project
coordination and technical assistance were provided by Mr. Philip J. Farrell and his staff at
Black, Crow and Eidsness, Inc.
The support of the project by the Water Quality Office, Environmental Protection Agency
and the assistance provided by Mr. Edmond Lomasney as Project Officer is acknowledged
with sincere thanks.
87
-------
SECTION XV
REFERENCES
Brosig, A. Jr., et al, "Activated Sludge Joint Treatment of Pulp and Paper Effluent with
Municipal Sewage," TAPPI, 54, 386 (1971).
Eckenfelder, William W., Industrial Water Pollution Control, McGraw-Hill Book Co., New
York.N. Y. (1966).
Eckenfelder, William W., Manual of Treatment Processes, Water Resource Management
Series, Vol. 1(1968).
Florida State Board of Health, Sewage Guide, 51-62 (1970).
Harnmerhill Paper Company and Erie, Pennsylvania, Joint Municipal and Semichemical
Pulping Waste Treatment, (July, 1969).
Spruill, E.L., "Paper Mill Waste: Treatment for Color Removal," Water and Sewage Works,
Vol. 118, No. 3, 82 (1971).
Wuhrmann, K., Advances in Biological Waste Treatment, Peigamon Press, Oxford (1963).
89
-------
SECTION XVI
GLOSSARY OF TERMS
Acid A compound which dissociates in water to form hydrogen ions.
Activated Sludge A flocculent assemblage of microorganisms, non-living organic matter
and inorganic materials.
Aeration Process of intimate contact between air and liquid device.
Aerobic Living only in the presence of free oxygen.
Alkalinity The ability of a water to accept proton, usually due to the presence of
bicarbonate, carbonate and/or hydroxide.
Bacteria One-celled microscopic organisms.
Batch Process A process in which there is no inflow or outflow.
Biochemical Oxygen Demand (BOD) - The quantity of oxygen utilized in the biochemical
oxidation of organic matterin 5 days at 20° C.
Biological Oxidation - A biochemical reaction in which materials combine with oxygen to
produce energy.
Buffer A substance in solution which makes the solution more resistant to pH changes.
Chemical Oxygen Demand (COD) The amount of oxygen required for the chemical
oxidation of organics in a liquid.
Chlorinator - A machine for feeding either liquid or gaseous chlorine to a stream of water.
Clarifier - A tank for separating solids in suspension by settling out.
C/N Ratio - The weight ratio of carbon to nitrogen in an organic system.
Coliform Organisms A group of bacteria recognized as indication of fecal pollution.
Colorimetric Determination - An analytical procedure based on measurement, or
comparison with standards, of color naturally present in samples or developed therein by
addition of reagents.
91
-------
Dehydrated Free from or lacking water.
Dilution Rate Reciprocal of retention time.
Dissolved Matter The material in solution in a liquid.
Dissolved Oxygen (DO) Oxygen not combined with other chemicals in water.
Effluent A liquid, solid or gas, frequently waste, discharged or emerging from a process.
Endogenous Respiration An auto-oxidation of cellular material that takes place in the
absence of assimilable organic material to furnish the energy required for the replacement of
worn-out components of protoplasm.
Equalizing Basin A holding basin in which, by retention, variations in flow and
composition of a liquid are averaged out.
Filtrate The liquid which has passed through a filter.
Filtration The process of separating solids from a liquid by means of a porous substance
through which only the liquid passes.
Floe A felted mass formed in a liquid medium by the aggregation of a number of fine
suspended particles.
Flow Diagram The diagrammatic representation of a works process, showing the sequence
and interdependence of the successive stages.
Flumed The transportation of solids by suspension in flowing water.
Hydrolysis A chemical reaction in which a compound reacts with the ions of water (H +-
OH") to form a weak acid, a weak base or both.
Limiting Nutrient That nutrient of which the concentration in the substrate limits the
growth of the organism utilizing the substrate.
Mixed Liquor Mixture of activated sludge and liquid waste.
Mixed Liquor Suspended Solids (MLSS) Filterable material contained in mixed liquor.
Mixed Liquor Volatile Suspended Solids (MLVSS) Filterable material in mixed liquor
which will ignite when exposed to 550° C. for one hour.
Nutrient Any substance assimilated by organisms which promotes growth and
replacement of cellular components.
92
-------
Oxidation Reaction of a substance with oxygen loss of electrons by one element to
another element.
Pathogenic Causing disease.
Residue That which remains after a part has been separated or otherwise treated.
Sedimentation Gravitational settling of solid particles in a liquid system.
Supernatant The liquid standing above a sediment or precipitate.
Thickening Tank A sedimentation tank for concentrated suspensions.
Total Suspended Solids (TSS) Total filterable solids in a sample.
Total Residue Total dissolved and suspended solids in a sample.
Turbidity - The reduction of transparency of a liquid due to the scattering of light by
suspended particles.
Unit Operation - A physical process which can be clearly distinguished from other
processes by the fundamental principles involved. Unlike most unit processes, unit
operations can be formulated in rather precise mathematical expressions.
Unit Process - A chemical or biological process which can be clearly distinguished from
other processes by the fundamental principles involved.
Symbols
C = Dissolved oxygen concentration at time, t
C* = Equilibrium dissolved oxygen concentration
t = time
W = Weight of water
KLa = Overall mass transfer coefficient
a = KLH (waste)
KLa (taP water)
0 = Ratio of saturation of DO in a waste to saturation of DO in
tap water at a given concentration
93
-------
SECTION XVH
APPENDIX
Table Number Page Number
A-1 Monthly Summary of Results of Overall Plant
Operation 96
A-2 Monthly Influent Wastewater Characteristics 97
A-3 Primary Treatment - Blend Tank (S-5) Effluent 99
A-4 Secondary Treatment Aeration Basin 101
A-5 Secondary Treatment - Aeration Basin Effluent 102
A-6 Secondary Treatment - Final Clarifier (S-9) 103
A-7 Secondary Treatment - Chlorine Contact Chamber (S-10) 104
95
-------
TABLE A-l
MONTHLY SUMMARY OF RESULTS OF OVERALL PLANT OPERATION*
Plant Influent
BOD Loading1
flb/davl
Date
1971
March
April
May
June
July
August
September
October
'November
December
1972
January
February
March
Ind.
186
188
177
201
201
304
323
255
478
423
365
302
Dom.
90
103
88
151
94
104
15
153
119
118
78
12
89
COD Loading1
(Ib/dav^l
Ind.
397
936
1,055
1,455
1,475
2,109
1,812
1,224
1,917
1,646
1,732
1,272
Dom.
243
260
229
435
286
302
61
409
302
345
189
31
272
PH
7.6
7.3
7.2
7.3
7.5
7.5
7.6
7.4
7.2
7.3
7.3
7.2
7.1
BOD Loading
(ib/day)
62
111
109
127
102
111
243
189
99
309
285
62
86
Chlorine Contact Chamber Effluent (S-10)
COD Loading
(Ib/day)
203
578
740
905
878
952
1,008
1313
976
1,535
1,247
348
766
Total
P04
(mg/1)
20
23
14
18
18
29
13
-
20
11
7
6
12
NH3 N03 N-Org. SS
(mg/1) (mg/1) (mg/1) (mg/1)
10.0 0.5 5.6
13.0 N.D. 10.5 295
144
170
141
121
- 154
264
- -497
- - 269
3.4 2 13.6 198
229
90
'Unclarified Waste
*Values represent monthly averages
N.D. - None Detected
-------
TABLE A-2
MONTHLY INFLUENT WASTEWATER CHARACTERISTICS*
BOD Loading1
(Ib/day)
Date
1971
March
April
May
June
July
August
September
October
November
December
1972
January
February
March
Ind.
186
167
128
204
213
350
379
281
474
510
395
335
Dom.
90
102
88
151
94
104
15
153
119
118
78
12
89
COD Loading1
(Ib/day)
Ind.
397
240
1,671
1,122
2,025
1,893
1,481
1,173
Dom.
243
260
229
435
286
302
61
409
302
345
189
31
272
pH
Ind.2
6.7
6.9
6.9
6.9
6.9
6.7
6.6
6.8
6.8
6.8
6.6
6.9
6.8
Dom.
7.1
7.0
6.8
6.9
7.0
6.8
6.8
6.8
6.7
6.9
6.9
6.9
6.8
Ortho PO4 (mg/1)
Ind.2
4
6
6
4
4
5
6
5
3
3
4
3
Dom.
14
18
19
31
28
34
28
24
12
8
12
Total PO4 (mg/1)
Ind.2
10
10
10
8
11
13
12
13
8
10
17
10
Dom.
23
24
20
29
29
36
32
33
20
19
18
1 Clarified Waste
2 Unclarified Waste
*Values represent monthly averages
N.D. - None Detected
-------
TABLE A-2 (Continued)
MONTHLY INFLUENT WASTEWATER CHARACTERISTICS*
Date
1971
March
April
May
June
July
August
September
October
November
December
1972
January
February
March
NH,
Ind.1
0.5
N.D.
0.1
1.0
5.2
2.7
1.6
(mg/1) NO,
Dom. Ind.1
12.0
19.7
18.3 N.D.
22.4 N.D.
23.0 N.D.
14.5
19.2 26
_ _
_ _
_
(mg/1)
Dom.
0.3
N.D.
N.D.
N.D.
N.D.
2.8
N-Org. (mg/1)
Ind.1
^
27.1
31.6
34.9
55.1
27.3
29.3
_
Dom.
7.0
11.1
8.9
9.4
9.1
8.6
7.0
Total Solids
(mg/1)
Ind.1
_
11,682
12,040
12,303
11,621
13,637
13,362
12,315
12,628
11,229
9,735
10,584
10,386
Dom.
_
427
401
499
501
615
528
551
562
444
394
432
382
Suspended Solids
(mg/1)
Ind.1
_
2,140
3,139
3,544
3,649
3,900
3,639
1,488
1,116
1,527
864
1,043
1,430
Dom.
_
83
36
63
83
79
76
78
105
52
70
86
40
^nclarified Waste
"Values represent monthly averages
N.D. - None Detected
-------
\O
TABLE A-3
PRIMARY TREATMENT - BLEND TANK (S-S) EFFLUENT*
Date
1971
March
April
May
June
July
August
September
October
November
December
1972
January
February
March
pH
_
7.3
7.2
7.2
7.1
7.1
7.2
7.1
7.2
7.2
7.4
7.2.
BOD
(mg/1)
...
333
223
264
237
1,266
439
431
514
510
616
371
COD
(mg/1)
1,035
1,281
1,362
1,376
5,105
1,594
1,665
1,689
1,573
1,848
1,307
Ortho
P04
(mg/1)
L
19
21
17
14
5
14
9
7
1
7
Total
PO4 NHj
(mg/l) (mg/1)
._.., ..
15 17.3
19 22.5
16 22.8
17 12.4
8 9.0
18
11
10
5
11
N03
(mg/l)
_
N.D.
N.D.
N.D.
13
_
N-Org.
(mg/l)
_
13.7
10.0
12.7
9.7
18.7
_
"Values represent monthly averages
N.D. - None Detected
-------
TABLE A-3 (Continued)
PRIMARY TREATMENT - BLEND TANK (S-5) EFFLUENT*
Date
1971
March
April
May
June
July
August
September
October
November
December
1972
January
February
March
Total
Solids
(mg/1)
1,638
1,282
1,764
2,008
6,823
1,989
1,976
2,238
2,031
2,827
1,665
Volatile
Solids
(mg/1)
Ill
612
881
941
2,717
888
885
872
859
963
727
Suspended
Solids
(mg/1)
380
170
278
312
1,210
123
191
243
158
110
140
Retention
Time(hr)
0.430
0.425
0.380
0.290
0.410
0.460
0.280
0.420
0.300
0.300
0.560
0.300
0.320
Nutrient
NH3 (Ib)
6.4
20.9
12.0
8.5
9.9
Feed
NH3 (ppm)
6.8
_
70
11.8
10.6
10.0
"Values represent monthly averages
N.D. - None Detected
-------
TABLE A-4
SECONDARY TREATMENT - AERATION BASIN*
Date
1971
March
April
May
June
July
August
September
October
November
December
1972
January
February
March
Retention
Time (hr)
13.8
15.0
25.0
21.2
26.0
30.5
67.1
25.6
29.5
20.2
22.6
30.3
22.7
SLR1
(Ib BOD/lb
MLVSS/day)
0.14
0.08
0.13
0.09
0.27
0.37
0.07
0.21
D.O.
Influent
(mg/1)
1.80
0.30
N.D.
0.10
0.19
0.11
0.64
0.77
0.65
2.90
2.70
2.20
Oa
Applied
(Ib)
9,709
12,740
10,920
11,160
12,650
12,700
13,468
14,720
13,826
11,590
14,100 .
12,600
ss
(mg/1)
145
553
899
2,448
4,591
4,050
7,069
3,430
3,233
2,146
2,240
2,328
1,820
vss
(mg/1)
ai_
622
2,068
3,237
3,402
5,509
2,915
3,107
1,959
1,870
2,045
1,580
1 Sludge Loading Rate
"Values Represent Monthly Averages
N.D. - None Detected
-------
TABLE A-5
SECONDARY TREATMENT - AERATION BASIN EFFLUENT*
Date
1971
March
April
May
June
July
August
September
October
November
December
1972
January
February
March
pH
7.5
7.3
7.3
7.2
7.4
7.4
7.5
7.2
7.2
7.2
7.2
7.2
7.1
BOD
(mg/i)
84
179
330
513
592
471
1,266
686
1,007
1,040
764
968
828
COD
(mg/1)
290
722
1,770
3,339
5,400
5,567
8,514
4,974
3,766
3,536
2,973
3,694
3,015
Ortlio
PH4
(mg/1)
14
21
22
34
23
20
16
16
9
7
2
8
Total
P04
(mg/1)
23
25
20
46
37
25
21
24
16
12
10
16
NH,
(mg/1)
10.0
16.0
5.2
12.6
10.1
5.4
4.4
6.8
9.3
11.4
3.2
6.0
7.6
NO,
(mg/1)
0.7
N.D.
N.D.
0.8
0.1
12.0
5.6
3.0
2.0
2.0
1.5
1.8
N-Org.
(mg/1)
7.5
8.2
17.0
28.0
24.2
15.7
34.9
71.0
172.0
104.2
48.2
79.4
29.2
Fixed
Solids
(mg/1)
433
1,513
1,294
1,363
1,250
~*~"
Total
Solids
(mg/1)
462
1,124
2,066
3,646
6,490
5',640
4,263
4,647
3,622
3,482
3,812
2,658
"Values represent monthly averages
N.D. - None Detected
-------
TABLE A-6
SECONDARY TREATMENT - FINAL CLARIFIER (S-9)*
8
Date
1971
March
April
May
June
July
August
September
October
November
December
1972
January
February
March
Retention
Time (hr)
1.9
2.1
3.7
3.0
3.7
2.6
4.3
1.9
2.1
1.8
1.9
2.7
2.2
pH
7.5
7.3
7.3
7.2
7.4
7.4
7.6
7.2
7.2
7.3
7.3
7.2
7.1
Ortho PO4
(mg/1)
14
19
16
21
20
18
11
13
8
6
0.6
8
Total PO4
(mg/1)
22
22
14
18
16
21
13
19
10
10
5
11
NH,
(mg/1)
12.0
14.6
7.6
12.0
16.5
5.2
4.8
8.3
9.3
8.7
2.7
4.9
8.0
NO3
(mg/1)
0.4
0.3
0.9
0.1
19.0
5.6
3.0
2.0
2.0
1.7
2.3
N-Org.
(mg/1)
6.3
8.0
17.4
11.5
13.1
9.0
17.3
21.5
24.6
18.0
13.9
23.1
11.4
VS
(mg/1)
.
525
588
550
699
766
1,866
705
571
684
643
881
418
SS
(mg/1)
308
237
186
156
175
192
286
276
294
200
284
150
"Values represent monthly averages
-------
g
TABLE A-7
SECONDARY TREATMENT - CHLORINE CONTACT CHAMBER (S-10)*
Date
1971
March
April
May
June
July
August
September
October
November
December
1972
January
February
March
Retention
Time (hr)
1.00
1.00
0.90
0.77
0.96
1.10
2.40
0.90
1.03
0.71
0.81
1.10
0.78
pH
7.6
7.3
7.2
7.3
7.5
7.5
7.6
7.4
7.2
7.3
7.3
7.2
7.1
BOD
(mg/1)
7.3
124
115
108
111
131
760
183
95
254
274
254
95
COD
(mg/1)
240
646
766
763
1,023
1,147
3,009
1,305
1,078
1,276
1,258
1,450
822
Ortho
P04
(mg/1)
12
19
15
23
22
22
11
17
10
6
0.4
8
Total
PO4 NHa NOj N-Org.
(mg/1) (mg/1) (mg/1) (mg/1)
20 10.0 0.5 5.6
23 13.0 N.D. 10.5
14
18
19
29
14
'
20
11
7 3.4 2.0 13.6
6
12
SS
(mg/D
295
144
170
141
121
154
264
497
269
198
229
90
Fixed
Solids
(mg/1)
_,_,
53
72
64
78
93
290
90
95
101
106
138
69
""Values represent monthly averages
N.D. - None Detected
-------
Subjeri Fn M fit Group
05D
SELECTED \VATicR RESOURCES ABSTRACTS
INPUT TRANSACTION FORM
J i Harriman Utility Board
Harriman, Tennessee
6 i T"'e Treatment of Domestic Wastewater and NSSC Pulp and Paper Mill Wastes
]Q \Authorfs)
' P. J. Farrell
L. R. Heble
A. G. Steuhser
16
Project Designation
EPA Project No. 11060 DBF
21
Note
A short appendix cohering the pilot plant's operational
parameters and results will be made available upon request.
22
Citation
Environmental Protection Agency report number,
EPA-660;2-73-010, December 1973.
23
Descriptors (Starred First)
*Domestic Waste, *Neutral Sulfite Semichemical (NSSC) Pulp and Paper Mill Waste, *PiIot Plant,
Primary Clarification, Biofiltration, Extended Aeration, Final Clarification, Disinfection
25
Identifiers (Starred First)
Joint Treatment, Organics Removal, Solids Removal, Color Removal
27 Abstract
The Harriman Utility Board and the Mead Corporation made a study of the joint treatment of
primary clarified domestic waste and neutral sulfite semichemical (NSSC) pulp and paper mill wastes.
A pilot plant was constructed and operated from April, 1971 through March, 1972.
The most effective treatment scheme consisted of a biofilter (used as a roughing filter) and an
extended aeration system. Color reduction was accomplished by massive lime and chlorine additions
due to the color's dependency on pH. Disinfection was optimum when ammonia was mixed with the
combined wastes prior to chlorination.
The biofilter's BOD removal efficiency ranged from 3 to 45 percent. Extended aeration's BOD
removal efficiency ranged from 24 to 98 percent.
This report was submitted in fulfillment of Research and Development Grant No. 11060-DBF
between the Environmental Protection Agency and the Harriman Utility Board, Harriman, Tennessee.
p_J-Farreli
Harriman utility Board, Harriman, Tennessee
WR:I02 (REV JULV 19691
«RSIC
SEND TO' WATER RESOURCES SCIENTIFIC INFORMATION CEf
U S DEPARTMENT OF THE INTERIOR
WASHINGTON. D C J0340
US. GOVERNMENT ff.OmtS SHCt IS/4- X6->U/19S
-------